JPH0328681A - Air separator - Google Patents
Air separatorInfo
- Publication number
- JPH0328681A JPH0328681A JP1166007A JP16600789A JPH0328681A JP H0328681 A JPH0328681 A JP H0328681A JP 1166007 A JP1166007 A JP 1166007A JP 16600789 A JP16600789 A JP 16600789A JP H0328681 A JPH0328681 A JP H0328681A
- Authority
- JP
- Japan
- Prior art keywords
- nitrogen
- nitrogen gas
- liquid
- liquefied
- heat exchanger
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 222
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 91
- 239000007788 liquid Substances 0.000 claims abstract description 45
- 229910001873 dinitrogen Inorganic materials 0.000 claims abstract description 42
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000001257 hydrogen Substances 0.000 claims abstract description 33
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 33
- 238000010992 reflux Methods 0.000 claims description 30
- 238000000926 separation method Methods 0.000 claims description 7
- 150000002829 nitrogen Chemical class 0.000 claims description 2
- 238000001816 cooling Methods 0.000 abstract description 12
- 238000010276 construction Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000003949 liquefied natural gas Substances 0.000 description 5
- 238000001179 sorption measurement Methods 0.000 description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- 239000003507 refrigerant Substances 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
- F25J3/0426—The cryogenic component does not participate in the fractionation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は精留塔から取出した窒素ガスを外部寒冷を用い
て液化させ、還流液として精留塔に戻す外部寒冷利用形
の空気分離装置に関するしのである。[Detailed Description of the Invention] [Industrial Application Field] The present invention provides an air separation device using external refrigeration, which liquefies nitrogen gas taken out from a rectification column using external refrigeration and returns it to the rectification column as a reflux liquid. This is a related story.
従来の外部寒冷利用形の空気分離装置の構成と作用を第
３図によって説明する。The structure and operation of a conventional air separation device using external refrigeration will be explained with reference to FIG.
原料空気濾過器１で濾過された原料空気は、原料空気圧
縮機２により吸着装置３での吸ｊ１操作を行なうのに必
要な圧力まで加圧され、吸着装置３で水分および二酸化
炭素等の不要成分を除去された後、コールドボックスＣ
に入る。４は予冷器、５は再生ガス加熱器である。The raw air filtered by the raw air filter 1 is pressurized by the raw air compressor 2 to the pressure required to perform the suction operation in the adsorption device 3, and the adsorption device 3 removes unnecessary moisture and carbon dioxide. After the components are removed, cold box C
to go into. 4 is a precooler, and 5 is a regeneration gas heater.
コールドボックスＣには、主熱交換器６および精留塔７
が設けられている。精留塔７は、原料空気圧力（約５Ｎ
！？／ｉｒｆｆｌＧ）で操作される高圧塔８と、これよ
りも低圧（ ０ ． ２ 〜０ ． ５ Ｋｇ／
ｃ！ｉＧ ）で操作される低圧塔９と、これら両塔８，
９間で熱交換を行なう主蒸化器１０とから戊っている。The cold box C includes a main heat exchanger 6 and a rectification column 7.
is provided. The rectification column 7 has a feed air pressure (approximately 5N
! ? /irfflG) and a lower pressure column (0.2 to 0.5 Kg/
c! iG), and both of these columns 8,
It is separated from the main evaporator 10 which performs heat exchange between the evaporators 9 and 9.
吸着装置３から出た原料空気は、主熱交換蒸６により沸
点近くまで冷却された後、精留塔７の高圧塔８に入り、
同塔内を上昇する間に還流液（戚体窒素）との接触によ
り次第に窒素濃度を高め、頂部では酸素含有量の少ない
窒素ガスとなる。The raw air coming out of the adsorption device 3 is cooled to near the boiling point by the main heat exchange steamer 6, and then enters the high pressure column 8 of the rectification column 7.
While rising in the column, the nitrogen concentration gradually increases due to contact with the reflux liquid (compound nitrogen), and at the top, the nitrogen gas becomes a nitrogen gas with low oxygen content.
この窒素ガスは主蒸化器１０に導入され、ここで液体酸
素との熱交換により凝縮して液体窒素となり、その一部
は低圧塔還流岐として低圧塔頂部に、また一部は高圧塔
還流液として高圧塔頂部にそれぞれ供給され、残りは製
品液体窒素として液体窒素タンク１１に抜き出される。This nitrogen gas is introduced into the main evaporator 10, where it is condensed into liquid nitrogen through heat exchange with liquid oxygen, and a portion of it is sent to the top of the low pressure column as a low pressure column reflux branch, and a portion is refluxed to the high pressure column. Each of these is supplied as a liquid to the top of the high-pressure column, and the remainder is withdrawn to the liquid nitrogen tank 11 as product liquid nitrogen.
上記高圧塔還流？夜は、高圧塔８内を下っていく間に空
気と接触して酸素濃度を高め、塔底から酸素３５〜４０
％を含む液体空気となって抜き出され、低圧塔中間部に
供給される。The above high pressure tower reflux? At night, while descending inside the high pressure column 8, it comes into contact with air and increases the oxygen concentration, and from the bottom of the column 35 to 40% of oxygen is released.
% of liquid air is extracted and supplied to the middle part of the low-pressure column.
この液体空気は、低圧塔９内を下降する間に酸素濃度を
増し、同塔底部から液体酸素が液体酸素タンク１２に抽
出される。また、低圧塔頂部から抜出された高純度窒素
ガスは、主熱交換器５により加熱された後、吸着装置３
に吸着塔再生ガスとして供給される。なお、低圧塔頂部
よりも少し下の低圧塔上部から低純度窒素ガスを取出し
、これを吸＠塔再生ガスとして使用してもよい。This liquid air increases its oxygen concentration while descending within the low-pressure column 9, and liquid oxygen is extracted from the bottom of the column into a liquid oxygen tank 12. Further, the high purity nitrogen gas extracted from the top of the low pressure column is heated by the main heat exchanger 5, and then heated by the adsorption device 3.
is supplied to the adsorption tower as regeneration gas. Note that low-purity nitrogen gas may be taken out from the upper part of the low-pressure column, which is slightly below the top of the low-pressure column, and used as the absorption column regeneration gas.
一方、高圧塔８の上部からは窒素ガスが窒素還流ライン
１３に取出され、この窒素還流ライン１３に設けられた
熱交換器１４で外部寒冷を与えられて液化した後、還流
液として高圧塔８の上部に戻される。On the other hand, nitrogen gas is taken out from the upper part of the high pressure column 8 to the nitrogen reflux line 13, and after being liquefied by external cooling in the heat exchanger 14 provided in the nitrogen reflux line 13, the nitrogen gas is sent to the high pressure column 8 as a reflux liquid. returned to the top.
上記従来の空気分離装置における窒素還流ライン１３の
熱交換器１４には、液化天然ガス（以下、ＬＮＧという
）が外部寒冷源として供給される。Liquefied natural gas (hereinafter referred to as LNG) is supplied as an external cooling source to the heat exchanger 14 of the nitrogen reflux line 13 in the conventional air separation device.
しかし、このＬＮＧの温度は、高圧塔８（塔内圧力が約
１９／ｃａｌＧ）での窒素の飽和温度（−１７６℃）よ
りも高い約−１５０℃であるため、高圧塔８から取出し
た窒素ガスをそのまま熱交換器１４で液化させることは
できない。However, since the temperature of this LNG is about -150°C, which is higher than the saturation temperature (-176°C) of nitrogen in high pressure column 8 (internal pressure of about 19/calG), the nitrogen taken out from high pressure column 8 Gas cannot be directly liquefied in the heat exchanger 14.
そこで従来は、図示のように窒素還流ライン１３におけ
る熱交換器１４の入口側に窒素圧縮機１５を設け、窒素
ガスをここで５０ｃａｌＧ以上の高圧まで圧縮すること
により窒素ガスの液化点を上げて熱交換器１４に入れ、
液化させるようにしている。Conventionally, a nitrogen compressor 15 is installed on the inlet side of the heat exchanger 14 in the nitrogen reflux line 13 as shown in the figure, and the nitrogen gas is compressed here to a high pressure of 50 calG or more to raise the liquefaction point of the nitrogen gas. put it in the heat exchanger 14,
I'm trying to liquefy it.
なお、図中、１６は熱交換器１４から出た液体窒素を高
圧塔８の圧力まで減圧するフラッシュボトルで、このフ
ラッシュボトル１６でガス化した窒素は窒素熱交換器１
７を通って窒素圧縮機１５に戻される。また、１８は窒
素還流ライン１３の窒素ガスを予冷する予冷器で、この
予冷器１８には、熱交換器１４で冷却された循環冷媒（
通常はフロン）が寒冷源として与えられる。１９はこの
冷媒用の循環ボンブ、２０はＬＮＧ加温器である。In the figure, 16 is a flash bottle that reduces the pressure of liquid nitrogen discharged from the heat exchanger 14 to the pressure of the high pressure column 8, and the nitrogen gasified in this flash bottle 16 is transferred to the nitrogen heat exchanger 1.
7 and returned to the nitrogen compressor 15. Further, 18 is a precooler for precooling the nitrogen gas in the nitrogen reflux line 13, and this precooler 18 is equipped with circulating refrigerant (
Freon (usually chlorofluorocarbons) is provided as a cooling source. 19 is a circulation bomb for this refrigerant, and 20 is an LNG warmer.
このように従来装置によると、熱交換器１５に窒素圧縮
機１５を組合わせて窒素ガスを液化させるようにしてい
るため、この圧縮機１５の分、動力が増加し、動力コス
トが高くなるという欠点があった。According to the conventional device, the nitrogen compressor 15 is combined with the heat exchanger 15 to liquefy the nitrogen gas, so the power required by the compressor 15 increases and the power cost increases. There were drawbacks.
そこで本発明は、精留塔から窒素還流ラインに取出した
窒素ガスを、加圧することなくそのまま液化させること
ができる空気分離装置を提供するものである。Therefore, the present invention provides an air separation device that can directly liquefy nitrogen gas taken out from a rectification column into a nitrogen reflux line without pressurizing it.
本発明は、精留塔内に発生する窒素ガスを窒素還流ライ
ンに取出し、この窒素還流ラインに設けられた液化手段
により液化させて精留塔に還流液として戻すように構成
される空気分離装置において、上記液化手段が、液体水
素を外部寒冷源とする熱交換装置によって構成されたも
のである（請求項１）。The present invention provides an air separation device configured to take out nitrogen gas generated in a rectification column to a nitrogen reflux line, liquefy it by a liquefaction means provided in the nitrogen reflux line, and return it to the rectification column as a reflux liquid. In this method, the liquefaction means is constituted by a heat exchange device using liquid hydrogen as an external cooling source (claim 1).
また、請求項２の発明は、請求項１の構成において、熱
交換装置が、精留塔から取出された窒素ガスとこの窒素
ガスよりも低圧の循環窒素との間で熱交換を行なう窒素
液化器と、上記循環窒素と液体水素との間で熱交換を行
なう水素・窒素熱交換器とによって構成されたものであ
る。Further, the invention of claim 2 is a nitrogen liquefaction system in which, in the structure of claim 1, the heat exchange device performs heat exchange between nitrogen gas taken out from the rectification column and circulating nitrogen having a pressure lower than that of the nitrogen gas. and a hydrogen/nitrogen heat exchanger that exchanges heat between the circulating nitrogen and liquid hydrogen.
このように、精留塔での窒素の飽和温度（高圧塔で−１
７６℃、低圧塔で−１９６℃）よりも低温（約−２０５
℃）の液体水素を外部寒冷源とする熱交換装置を用いる
ことにより、精留塔から取出した窒素ガスを圧縮機で加
圧することなくそのまま熱交換装置によって液化させる
ことができる。In this way, the saturation temperature of nitrogen in the rectification column (-1
76°C (-196°C in the low pressure column) (approximately -205°C)
By using a heat exchange device that uses liquid hydrogen at temperatures (°C) as an external cooling source, the nitrogen gas taken out from the rectification column can be directly liquefied by the heat exchange device without being pressurized by a compressor.
従って、窒素圧縮機が不要となる分、動力を低減でき、
動力コストを安くすることができる。Therefore, the power can be reduced by eliminating the need for a nitrogen compressor.
Power costs can be reduced.
また、請求項２の構成によると、液体水素と窒素ガスと
が循環窒素を介して間接的に熱交換するため、熱交換装
置での漏れによって液体水素が液体窒素とともに精留塔
に入る危険性がない。Further, according to the structure of claim 2, since liquid hydrogen and nitrogen gas indirectly exchange heat through circulating nitrogen, there is a risk that liquid hydrogen will enter the rectification tower together with liquid nitrogen due to a leak in the heat exchange device. There is no.
本発明の実施例を第１図および第２図によって説明する
。An embodiment of the present invention will be described with reference to FIGS. 1 and 2.
以下の実施例では、第３図に示す従来装置と同一部分に
は同一符号を付して示し、その重複説明を省略する。In the following embodiments, parts that are the same as those of the conventional device shown in FIG. 3 are denoted by the same reference numerals, and redundant explanation thereof will be omitted.
第１実施例（第１図参照）
窒素還流ライン２１は、従来同様、入口側が精留塔７に
おける高圧塔８の上部に接続され、高圧塔８内の窒素ガ
スがこの窒素還流ライン２１に取出される。First embodiment (see Fig. 1) As in the conventional case, the inlet side of the nitrogen reflux line 21 is connected to the upper part of the high pressure column 8 in the rectification column 7, and the nitrogen gas in the high pressure column 8 is taken out to this nitrogen reflux line 21. be done.
窒素還流ライン２１には熱交換装置２２が設けられ、上
記取出された窒素ガスがこの熱交換装置２２に直接、す
なわち圧縮機で加圧されずにそのまま導入される。A heat exchange device 22 is provided in the nitrogen reflux line 21, and the nitrogen gas taken out is directly introduced into this heat exchange device 22, that is, without being pressurized by a compressor.
この熱交換装置２２は、高圧塔８からの窒素ガス（以下
、被液化窒素ガスという）よりも低い圧力をもって窒素
が閉サイクルで循環する窒素閉ライン２３と、外部寒冷
源としての液体水素が通される水素ライン２４とを有し
、水素ライン２ ４と窒素閉ライン２３とに跨って水素
・窒素熱交換器２５、窒素閉ライン２３と窒素還流ライ
ン２１とに跨って窒素液化器２６がそれぞれ設けられて
いる。２７は窒素閉ライン２４に設けられた窒素循環ポ
ンプ、２８は窒素還流ライン２１における窒素液化器２
６の出口側に設けられた還流ポンプである。This heat exchange device 22 has a nitrogen closed line 23 in which nitrogen is circulated in a closed cycle at a pressure lower than that of nitrogen gas (hereinafter referred to as liquefied nitrogen gas) from the high pressure column 8, and liquid hydrogen as an external cooling source communicates with each other. A hydrogen line 24 is provided, a hydrogen/nitrogen heat exchanger 25 is provided astride the hydrogen line 24 and the nitrogen closed line 23, and a nitrogen liquefier 26 is provided astride the nitrogen closed line 23 and the nitrogen reflux line 21. It is provided. 27 is a nitrogen circulation pump installed in the nitrogen closed line 24, and 28 is a nitrogen liquefier 2 in the nitrogen reflux line 21.
This is a reflux pump installed on the outlet side of 6.
この構成において、被液化窒素ガスの圧力をたとえばＩ
Ｎｇ／ａｉＡ，窒素閉ライン２３を流れる循環窒素の圧
力を０．６Ａｇ／ｃｄＡとすると、循Ｆｉ窒素は約−２
００℃で凝縮・蒸発する。従って、この循環窒素は、水
素・窒素熱交換器２５で約−２０５℃の液体水素との熱
交換によって凝縮する。In this configuration, the pressure of the nitrogen gas to be liquefied is set to, for example, I
Ng/aiA, if the pressure of the circulating nitrogen flowing through the nitrogen closed line 23 is 0.6Ag/cdA, the circulating Fi nitrogen is approximately -2
Condenses and evaporates at 00℃. Therefore, this circulating nitrogen is condensed in the hydrogen/nitrogen heat exchanger 25 by heat exchange with liquid hydrogen at about -205°C.
そして、この液体窒素は窒素液化器２６の低温部に送ら
れ、ここで披液化窒素ガスとの熱交換によって蒸発し、
被液化窒素ガスは液化する。Then, this liquid nitrogen is sent to the low temperature section of the nitrogen liquefier 26, where it is evaporated by heat exchange with the liquid nitrogen gas.
The nitrogen gas to be liquefied is liquefied.
こうして、液体水素の寒冷が循環窒素を介して被液化窒
素ガスに間接的に与えられて同ガスが液化し、還流ボン
ブ２８により精留塔７の高圧塔上部に還流液として戻さ
れる。In this way, the cooling of the liquid hydrogen is indirectly applied to the nitrogen gas to be liquefied through the circulating nitrogen, the gas is liquefied, and is returned to the upper part of the high-pressure column of the rectification column 7 as a reflux liquid by the reflux bomb 28.
このように本装置によると、高圧塔８での窒素の飽和温
度（−１７６℃）よりも低温（−２０５℃）の液体水素
を外部寒冷源とする熱交換装置２２を用いることにより
、精留塔７から取出した窒素ガスを、第３図に示す従来
装置の場合のように圧縮機１５で加圧して液化点を上げ
る必要がなくなり、窒素ガスをそのまま熱交換装置２２
で液化させることができる。従って、圧縮機１５を省略
できる分、動力を低減化でき、動力コストを安くするこ
とができる。As described above, according to this device, by using the heat exchange device 22 which uses liquid hydrogen at a temperature lower than the saturation temperature (-176°C) of nitrogen in the high-pressure column 8 (-205°C) as an external cooling source, the rectification can be carried out. It is no longer necessary to pressurize the nitrogen gas taken out from the column 7 with the compressor 15 to raise the liquefaction point as in the case of the conventional apparatus shown in FIG.
It can be liquefied. Therefore, since the compressor 15 can be omitted, the power can be reduced and the power cost can be reduced.
また、熱交換装置２２において、液体水素の寒冷を循環
窒素を介して窒素ガスに間接的に与えるため、この熱交
換装置２２での漏れによって水素が窒素還流ライン２１
に流れ込み、酸素を生産している精留塔７に侵入する危
険性がない。In addition, in the heat exchange device 22, since the cooling of liquid hydrogen is indirectly applied to the nitrogen gas through the circulating nitrogen, hydrogen is transferred to the nitrogen reflux line 22 due to leakage in the heat exchange device 22.
There is no risk of the gas flowing into the rectifying column 7 where oxygen is produced.
さらに、間接冷媒である循環窒素が閉ライン２３中で−
１８０℃〜−２０５℃の温度レヘルで蒸発・凝縮するた
め、潜熱を熱交換に利用することができる。すなわち、
他のガスや液体等、単一相の顕熱での熱交換と比較して
、熱交換装置２２での温度差を小さくすることが可能と
なるため、エネルギーのロスが小さくなり、熱交換装置
２２を小さくすることができる。Furthermore, circulating nitrogen, which is an indirect refrigerant, is circulated in the closed line 23.
Since it evaporates and condenses at a temperature range of 180°C to -205°C, latent heat can be used for heat exchange. That is,
Compared to heat exchange using single-phase sensible heat such as other gases or liquids, it is possible to reduce the temperature difference in the heat exchange device 22, so energy loss is reduced and the heat exchange device 22 can be made smaller.
第２実施例（第２図参照） 第１実施例との相違点のみを説明する。Second embodiment (see Figure 2) Only the differences from the first embodiment will be explained.
第２実施例は、精留塔７での液体窒素の生産量が液体酸
素の生産量よりも多い場合（たとえばｉｆｋ体酸素生産
量と液体窒素の生産瓜との比率が１２〜３の場合）のプ
ロセスを示している。In the second embodiment, when the production amount of liquid nitrogen in the rectification column 7 is larger than the production amount of liquid oxygen (for example, when the ratio of the production amount of ifk body oxygen to the production amount of liquid nitrogen is 12 to 3) It shows the process of
この場合は、窒素ガスが精留塔７における低圧塔９の頂
部から窒素還流ライン２１に取出され、熱交換装置２２
により液化された後、低圧塔頂部に還流液として戻され
る。In this case, nitrogen gas is taken out from the top of the low pressure column 9 in the rectification column 7 to the nitrogen reflux line 21, and the heat exchanger 22
After being liquefied, it is returned to the top of the low-pressure column as a reflux liquid.
この第２実施例の場合も、同じプロセスをとる従来装置
で必要であった、低圧窒素ガスを圧縮してＬ Ｎ Ｇ熱
交換器で液化可能な圧力まで加圧するための圧縮機が不
要となる。This second embodiment also eliminates the need for a compressor to compress low-pressure nitrogen gas to a pressure that can be liquefied in the LNG heat exchanger, which was required in conventional equipment that uses the same process. .
その他の実施例
（１）液体水素を外部寒冷源として用いるこの装置にお
いては、精留堪７内への峡体水素の侵入をトノノ止する
ために上記実施例のように窒素閉ライニ、２３を介して
液体水素と窒素ガスとを間接的に熱交換させる構成をと
るのが望Ｉしいが、熱交換装置２２での液体水素の漏れ
対策が万全な場合には、ｉ＆体水素と窒素ガスとを直接
熱交換させるように構成してもよい。Other Embodiments (1) In this apparatus using liquid hydrogen as an external cooling source, the nitrogen-closed liner 23 is installed as in the above embodiment in order to prevent the isthmic hydrogen from entering into the rectification chamber 7. It is desirable to adopt a configuration in which liquid hydrogen and nitrogen gas are indirectly heat exchanged through It may also be configured to directly exchange heat.
＜Ｉ１）上記両実施例では、水素・窒素熱交換器２５で
ｊ（ｌられた液体窒素を窒素液化器２６に移送じ、また
窒素液化器２６で得られた液体窒素を精留塔７に戻すた
めにそれぞれボンブ２７，２８を用いたが、水素・窒素
熱交換器２５を窒素液化器２ ６よりも丁｛ｂい位置に
、また窒素液化器２６を精留塔゛７における還流岐流入
位置（第１実施例の場合は高圧塔８の上部、第２尖施例
の場合は低圧塔（）の１￥ｉ部）よりも商い位置にそれ
ぞれ設置できる場Ａには、液ヘッドによって液体窒素を
窒素液化器２６または桔留塔７に移送ずることができる
ため、これらボンブ２７，２Ｂは不要となる。<I1) In both of the above embodiments, the liquid nitrogen produced by the hydrogen/nitrogen heat exchanger 25 is transferred to the nitrogen liquefier 26, and the liquid nitrogen obtained in the nitrogen liquefier 26 is transferred to the rectification column 7. Bombs 27 and 28 were used for the return, but the hydrogen/nitrogen heat exchanger 25 was placed at a position slightly lower than the nitrogen liquefier 26, and the nitrogen liquefier 26 was placed at the reflux branch inlet of the rectification column 7. In place A, which can be installed at a position lower than the position (in the case of the first embodiment, the upper part of the high-pressure column 8, in the case of the second embodiment, the part of the low-pressure column ()), the liquid is Since the nitrogen can be transferred to the nitrogen liquefier 26 or the distillation tower 7, these bombs 27 and 2B are no longer necessary.
上記のように本発明によるときは、精留塔での窒素の飽
和温度よりも低温の液体水素を外部寒冷源とする熱交換
装置を用いることにより、精留堪から取出した窒素ガス
を圧縮機で加圧することなくそのまま熱交換装置によっ
て液化させることができる。このため、窒素圧縮機が不
要となる分、動力を低減でき、動力コストを安くするこ
とができる。As described above, according to the present invention, by using a heat exchange device using liquid hydrogen at a temperature lower than the saturation temperature of nitrogen in the rectifier as an external cold source, the nitrogen gas extracted from the rectifier is transferred to the compressor. It can be directly liquefied using a heat exchanger without pressurizing it. Therefore, since a nitrogen compressor is not required, the power can be reduced and the power cost can be reduced.
また、請求項２の発明によると、液体水素と室素ガスと
が循環窒素を介して間接的に熱交換するため、熱交換装
置での漏れによって液体水素が液体窒素とともに情留塔
に侵入する危険性がない。Further, according to the invention of claim 2, since the liquid hydrogen and the nitrogen gas indirectly exchange heat through the circulating nitrogen, the liquid hydrogen enters the distillation tower together with the liquid nitrogen due to a leak in the heat exchange device. There is no danger.
第１図は本発明の第１実施例、第２図は同第２実施例、
第３図は従来装置をそれぞれ示すフローシ一トである。
７・精留塔、８・・・精留塔の高圧塔、９・・・同低圧
堵、：２１・・・窒素還流ライン、２２・・・熱交換装
置、２５・同熱交換装置における水素・窒素熱交換器、
２６・・・同窒素液化器。FIG. 1 shows a first embodiment of the present invention, FIG. 2 shows a second embodiment of the invention,
FIG. 3 is a flowchart showing each conventional device. 7. Rectifying column, 8... High pressure column of the rectifying column, 9... Low pressure column of the rectifying column, 21... Nitrogen reflux line, 22... Heat exchange device, 25. Hydrogen in the same heat exchange device・Nitrogen heat exchanger,
26...Nitrogen liquefier.
Claims (1)
の窒素還流ラインに設けられた液化手段により液化させ
て精留塔に還流液として戻すように構成される空気分離
装置において、上記液化手段が、液体水素を外部寒冷源
とする熱交換装置によって構成されたことを特徴とする
空気分離装置。 ２、熱交換装置が、精留塔から取出された窒素ガスとこ
の窒素ガスよりも低圧の循環窒素との間で熱交換を行な
う窒素液化器と、上記循環窒素と液体水素との間で熱交
換を行なう水素・窒素熱交換器とによって構成されたこ
とを特徴とする請求項１記載の空気分離装置。[Scope of Claims] 1. Air configured to take out nitrogen gas in the rectification column to a nitrogen reflux line, liquefy it by a liquefaction means provided in this nitrogen reflux line, and return it to the rectification column as a reflux liquid. An air separation device characterized in that the liquefaction means is constituted by a heat exchange device using liquid hydrogen as an external cold source. 2. A heat exchange device exchanges heat between the nitrogen gas taken out from the rectification column and circulating nitrogen at a lower pressure than this nitrogen gas, and a nitrogen liquefier that exchanges heat between the circulating nitrogen and liquid hydrogen. 2. The air separation apparatus according to claim 1, further comprising a hydrogen/nitrogen heat exchanger for performing the exchange.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1166007A JP2582438B2 (en) | 1989-06-27 | 1989-06-27 | Air separation equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1166007A JP2582438B2 (en) | 1989-06-27 | 1989-06-27 | Air separation equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0328681A true JPH0328681A (en) | 1991-02-06 |
| JP2582438B2 JP2582438B2 (en) | 1997-02-19 |
Family
ID=15823161
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1166007A Expired - Fee Related JP2582438B2 (en) | 1989-06-27 | 1989-06-27 | Air separation equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2582438B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101619917A (en) * | 2008-06-30 | 2010-01-06 | 普莱克斯技术有限公司 | Nitrogen liquefier retrofit for air separation plant |
| EP4343247A1 (en) * | 2022-09-23 | 2024-03-27 | Messer SE & Co. KGaA | Method and apparatus for producing air gases |
| JP2024543279A (en) * | 2022-10-12 | 2024-11-21 | コリア ガス コーポレーション | Rare gas production system and liquefied hydrogen receiving terminal including the same |
| EP4446680A3 (en) * | 2023-04-11 | 2025-01-01 | Messer SE & Co. KGaA | Method and device for liquefying gases |
| EP4517238A1 (en) * | 2023-08-31 | 2025-03-05 | Linde GmbH | Method and apparatus for providing liquid air products |
| WO2025224970A1 (en) * | 2024-04-26 | 2025-10-30 | 川崎重工業株式会社 | Cryogenic separation device |
| WO2025224969A1 (en) * | 2024-04-26 | 2025-10-30 | 川崎重工業株式会社 | Cryogenic separation device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP6244190B2 (en) | 2013-11-29 | 2017-12-06 | 株式会社吉野工業所 | Foam discharge container |
-
1989
- 1989-06-27 JP JP1166007A patent/JP2582438B2/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101619917A (en) * | 2008-06-30 | 2010-01-06 | 普莱克斯技术有限公司 | Nitrogen liquefier retrofit for air separation plant |
| EP4343247A1 (en) * | 2022-09-23 | 2024-03-27 | Messer SE & Co. KGaA | Method and apparatus for producing air gases |
| JP2024543279A (en) * | 2022-10-12 | 2024-11-21 | コリア ガス コーポレーション | Rare gas production system and liquefied hydrogen receiving terminal including the same |
| EP4446680A3 (en) * | 2023-04-11 | 2025-01-01 | Messer SE & Co. KGaA | Method and device for liquefying gases |
| EP4517238A1 (en) * | 2023-08-31 | 2025-03-05 | Linde GmbH | Method and apparatus for providing liquid air products |
| WO2025224970A1 (en) * | 2024-04-26 | 2025-10-30 | 川崎重工業株式会社 | Cryogenic separation device |
| WO2025224969A1 (en) * | 2024-04-26 | 2025-10-30 | 川崎重工業株式会社 | Cryogenic separation device |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2582438B2 (en) | 1997-02-19 |
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